Classifications

• • C—CHEMISTRY; METALLURGY
  • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
  • C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
  • C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
  • C25C7/02—Electrodes; Connections thereof
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F1/00—Treatment of water, waste water, or sewage
  • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
  • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
  • C02F1/46104—Devices therefor; Their operating or servicing
  • C02F1/46109—Electrodes
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F1/00—Treatment of water, waste water, or sewage
  • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
  • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
  • C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
  • C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F1/00—Treatment of water, waste water, or sewage
  • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
  • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
  • C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
  • C02F1/4676—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electroreduction
  • C02F1/4678—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electroreduction of metals
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F1/00—Treatment of water, waste water, or sewage
  • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
  • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
  • C02F1/46104—Devices therefor; Their operating or servicing
  • C02F1/46109—Electrodes
  • C02F2001/46133—Electrodes characterised by the material
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F1/00—Treatment of water, waste water, or sewage
  • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
  • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
  • C02F1/46104—Devices therefor; Their operating or servicing
  • C02F1/46109—Electrodes
  • C02F2001/46152—Electrodes characterised by the shape or form
  • C02F2001/46157—Perforated or foraminous electrodes
  • C02F2001/46161—Porous electrodes
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F2101/00—Nature of the contaminant
  • C02F2101/10—Inorganic compounds
  • C02F2101/16—Nitrogen compounds, e.g. ammonia
  • C02F2101/18—Cyanides

Definitions

• the subject of the invention is a porous percolating fibrous electrode modified with carbon or graphite. It also relates to the application of such an electrode to the performance of electrochemical reactions and in particular to the electrodeposition of metals contained in the form of ions in various industrial liquids. Finally, it relates to electrochemical reactors with percolating porous electrodes for which the percolating porous electrodes are of the type of said modified fibrous percolating porous electrode.
• Electrodes with a large specific surface called porous electrodes. percolating.
• Such electrodes are in the form of a porous matrix of a conductive material or in a mixture of a conductive material and a non-conductive material.
• the percolating porous electrode is opposite to a counter-electrode and the effluent to be treated, which plays the role of electrolyte , is caused to percolate through the percolating porous electrode.
• the electrochemical reaction in this case the reduction of metal ions to metal, due to the potential difference between the matrix of the porous electrode and the solution which is in relation to the potential difference established between the percolating porous electrode and the counter electrode takes place within said porous percolating electrode.
• porous percolating electrodes with a fibrous carbon or graphite structure which combine the various advantages of porous percolating electrodes and furthermore are considerably less costly than the electrodes.
• porous percolating with a non-fibrous structure The porous percolating fibrous electrodes known from carbon or graphite are for example made up of carbon fibers arranged in a specific manner (American patent No. 4,046,663) or else can consist of a graphite fabric (D. Yaniv and M. Ariel: “ Electrodeposition and Stripping at Graphite Cloths Electrodes ", Journal of Electroanalytical Chemistry, 79 (1977), pages 159-167).
• porous percolating fibrous carbon or graphite electrodes lie in the fact that they give results which do not have satisfactory reproducibility and generally low yields.
• the invention provides a porous percolating fibrous electrode modified in carbon or graphite which overcomes the aforementioned drawbacks and remains of a cost comparable to that of the corresponding unmodified percolating porous electrode.
• the porous fibrous percolating electrode according to the invention is of the type comprising a porous fibrous matrix of carbon or graphite and it is characterized in that said matrix is a modified matrix which results from the impregnation of a porous fibrous matrix of carbon or graphite by a solution containing 0.01% to 1% by weight of a surfactant, so that said modified matrix has in the wet state an apparent density with respect to water having a value between 1 , 6 and 3 times the value of the apparent density relative to the water of the unmodified fibrous porous matrix corresponding to the wet state.
• the porous fibrous matrix modified in carbon or graphite of the porous percolating fibrous electrode has in the wet state an apparent density with respect to water having a value ranging from 1.8 to 2.7 times the value of the apparent density with respect to the water of the unmodified fibrous porous matrix corresponding to the wet state.
• the term "apparent density with respect to water of the porous fibrous matrix in the wet state" means the ratio of the mass of a certain volume of the porous fibrous matrix, after immersion in water for a period of between 1 and 2 minutes, to the mass of the same volume of water.
• the ratio 8, - & has, according to the invention, a value between 1.6 and 3 and preferably ranging from 1.8 to 2.7.
• a surfactant is meant both a surfactant and a mixture of surfactants.
• the technique of impregnating the fibrous matrix with the surfactant is not critical.
• the surfactant concentration of the surfactant solution used to impregnate the porous fibrous matrix is between 0.01% and 1% of the weight of said solution.
• Aqueous solutions of the surface-active agent containing more than 1% by weight of surface-active agent do not bring additional improvements and in addition the quantity of surface-active agent deposited from such solutions within of the porous fibrous matrix causes annoying foaming when the modified percolating porous electrode is brought into contact with the effluent to be treated electrochemically.
• the surfactants which can be used to constitute the agent for impregnating the fibrous matrix of the percolating porous electrode can be anionic, cationic, nonionic or even amphoteric surfactants.
• anionic surfactants that may be mentioned are sulfated glycerides, sulfated esters and, for example, sulfated alkyl oleates such as sulfated butyl oleate, olefins with long sulfated chains, sulfates of saturated or unsaturated fatty alcohols saturated and for example sodium lauryl sulphate, sodium cetyl sulphate, sodium 2-ethyl hexyl sulphate, sodium sulphate of oleic alcohol, alkane sulphonates of alkali metals and in particular sodium alkanesulphonates, sulphosuccinates , alkali metal sulfonates of alkali metals and in particular sodium alkylna
• the cationic surfactants can be chosen, among others, from fatty amine hydrochlorides or also from quaternary ammonium chlorides of long chain amines such as, for example, lauryltrimethylammonium chloride or laurylpyridinium chloride.
• nonionic surfactants that may be mentioned, for example, are the products of addition of ethylene oxide to alcohols or phenols and in particular the polyoxyethylene ethers of higher fatty alcohols and the polyoxyethylene ethers of alkylphenols, or also esters fatty acids of polyoxyalkylene glycols and in particular fatty acid esters of polyoxyethylene glycols.
• amphoteric surfactants it is possible to use, for example, amino acids and betaines having long chain alkyl residues, or alternatively sulphates of unsaturated or hydroxylated fatty amines and for example sulphated oleylamine or sulfated hydroxyoctadecylamine.
• the surfactant impregnating the fibrous matrix of the percolating porous electrode has a number representative of its hydrophilic / lipophilic balance (in English "HLB number") between 5 and 20 and more particularly located between 10 and 16.
• the porous fibrous carbon or graphite matrix from which is formed, for example by impregnation by means of a surfactant, the modified porous fibrous matrix of the percolating porous electrode according to the invention can be formed by any structure carbon or graphite fiber having sufficient porosity for a solution to percolate through this structure under the conditions usually required for porous percolating electrodes.
• Said porous fibrous matrix may consist, for example, of a structure of carbon fibers, in particular of the type described in American patent No. 4,046,663, or of a woven or non-woven fabric of carbon or graphite, or even of fluff carbon fibers or graphite.
• said fibrous matrix of the percolating porous electrode is a carbon or graphite felt.
• the percolating porous electrode modified according to iriventoin may be in the form of a plate or a wafer, a disc, or may have an annular shape or any other desired shape.
• the modified percolating porous electrode according to the invention finds in particular an application as a percolating porous electrode for carrying out electrochemical reactions, and more particularly for carrying out electrochemical reactions in aqueous phase, using the process in which a solution containing the or the species liable to react electrochemically, is caused to percolate through the porous electrode, said solution being traversed by an electric current resulting from the establishment of a potential difference between said electrode porous percolating agent and a counter electrode, which may also be a porous percolating electrode, in contact with the solution.
• the aforementioned process using the percolating porous electrode according to the invention can be used in particular for the recovery by electrodeposition of metals, in particular copper, lead, silver, gold, mercury, cadmium, nickel, contained in varying concentrations under the form of ions in various solutions, for example in low concentrations in industrial effluents or in higher concentrations in solutions of hydrometallurgical treatments.
• the aforementioned process can also be used for the destruction of certain organic pollutants or of certain anions such as the cyanide ions contained in the waste waters of certain treatments, or even for carrying out syntheses of organic products comprising one or more electrochemical reactions.
• electrochemical cells or reactors which can be used to carry out such electrochemical reactions according to the invention are of the type of electrochemical cells or reactors with fixed percolating porous electrodes known in the art, for which however the percolating porous electrode is a modified percolating porous electrode according to the invention.
• Such electrochemical cells or reactors generally comprise an enclosure provided with an inlet and an outlet for the solution to be treated, a fixed percolating porous electrode disposed in said enclosure in the vicinity of the inlet so that the liquid supplied to the entry of the enclosure enters the latter only by percolation through said electrode, a counter electrode placed in the enclosure between the porous percolating electrode and the outlet of said enclosure, means for establishing a potential difference between said electrodes and means for circulating the solution to be treated from the inlet to the outlet of the enclosure.
• the porous percolating electrode and the counter electrode which can also be a porous percolating electrode, can be arranged so that the lines of current in the solution between the electrodes are parallel to the direction of flow of said solution or that said streamlines are substantially orthogonal to the direction of flow of the solution.
• electrochemical cells or reactors analogous to those represented schematically in American patent No. 4,046,663, or in the article by GA Carlson and EE Estep entitled: "Porous Cathode Cell for Metals Removal from Aqueous Solutions” and published in Electrochemical Contributions to Environmental Protection, 1972, pages 159 to 167, or in the article by GA Carlson, EE Estep, and D. Jacqueau entitled: “Porous Cathode Cell for Sodium Hydroxide Purification” and published in the journal Chemie- Engineer-Technik, 1973, 45 (4), pages 217 to 219.
• Mechanical regeneration is to be considered when the solid deposit, in particular metallic deposit, is preferably on the surface of the percolating porous electrode, said regeneration being able to be carried out for example by detaching the deposited product, in particular metal, by gravity by stopping the 'liquid supply to the cell or the electrochemical reactor or by scraping the surface of the porous percolating electrode continuously or discontinuously.
• said electrode is brought into contact with a minimum volume of a reagent suitable for dissolving the solid deposited in the electrode and to obtain a concentrated solution of the product dissolved in said reagent.
• this re-solution corresponds to an electrochemical oxidation of the deposited metal and to do this, the percolating porous electrode clogged by the deposit plays the role of anode and the counter-electrode the role cathode.
• an electrochemical cell or reactor consisting of a enclosure comprising an inlet in its middle part and a first and a second outlet on either side of this inlet, a first porous percolating fixed electrode mounted in the enclosure between the inlet and one of the outlets and a second electrode porous percolating fixed between said inlet and the other outlet, said porous percolating electrodes being arranged in the enclosure so that the solution to be treated, circulating in the enclosure of the inlet to each of the outlets, percolates through each of said electrodes, means for establishing a potential difference between the electrodes, one of the electrodes acting as an anode and the other cathode, and means for bringing the solution to be treated and for circulating it from the input to the outputs of the enclosure.
• Such a cell is similar to that schematically represented in the article by DN Bennion and J. Newman entitled: "Electrochemical Removal of Copper Ions from Very Dilute Solutions” and published in Journal of Applied Electro-chemistry 2 (1972), pages 113 to 122, however with the use of porous percolating electrodes modified according to the invention.
• the metal is deposited within the percolating porous electrode playing the role of cathode, and to regenerate the cathode charged with the deposited metal, the role is swapped played by the electrodes by reversing their polarity.
• the potential to be imposed on the percolating porous electrode or to be established between the electrodes of the reactor or of the electrochemical cell can be deduced from the intensity / potential curve determined experimentally for the reaction in which one is interested carried out in the chosen reactor, or a reactor of the same geometry, on the solution to be treated.
• the potential to be imposed on the porous percolating electrode generally corresponds to a value of the potential chosen on the level of the limit diffusion current, and the potential to be established between the electrodes of the cell or of the electrochemical reactor is related to this value by taking also account for the ohmic drop in the solution between the electrodes.
• the speed of passage of the solution to be treated in the cell or the electrochemical reactor is chosen to obtain a satisfactory yield for the electrochemical reaction which is carried out while avoiding undesirable phenomena, for example the clogging of the percolating porous electrode in the case where the electrochemical reaction leads to a solid deposit within or / and on the porous percolating electrode.
• These operating conditions correspond substantially to those used to carry out the electrochemical reaction in the cell or the electrochemical reactor corresponding to that used according to the invention but equipped with an unmodified percolating porous electrode.
• a disc of commercial carbon felt having a thickness of 4 millimeters was impregnated with a surfactant based on alkyl sulfates known commercially under the name of TEEPOL and having an HLB value of between 13 and 15.
• the impregnation was carried out by immersing the felt disc in a 0.1% aqueous solution of the surfactant, then quickly rinsing it with distilled water and allowing it to drain.
• the disc impregnated with the surfactant had an apparent density in the wet state relative to water (8M) equal to 1.03.
• the ratio of the apparent density 8M of the felt impregnated in the wet state to the apparent density 80 of the felt not impregnated in the wet state was 2.56.
• the electrolytic cell used consisted of a vertical cylindrical enclosure closed at each of its ends and provided at its lower end with an inlet for the solution to be treated and at its upper part with an outlet for the purified solution.
• the percolating porous electrode acted as a cathode.
• a platinum electrode was placed in the upper compartment of the cell and a potassium nitrate salt bridge connected the said cell to a reference electrode to the calomel.
• Each of the electrodes was connected to a potentiostat making it possible to impose a DC electrical voltage of known value on the cathode and on the anode.
• a millivoltmeter made it possible to measure the potential difference between the cathode and the reference electrode and a milliammeter was connected in series with the anode on the circuit connecting this anode to the potentiostat.
• the entrance to the electrolytic cell was connected, through a peristaltic pump, to a reservoir containing the solution to be treated.
• An electrolysis potential (electrochemical reduction reaction of cupric metal ions) was imposed on the cathode equal to -300 millivolts (relative to the reference electrode), this value being determined on the intensity / potential curve established experimentally for the solution considered and representing the average potential of the potential interval corresponding to the level of the curve defining the limit diffusion current.
• the cupric solution was injected into the electrolysis cell by the peristaltic pump in such a way that it percolated through the percolating porous electrode and circulated in said cell with a constant speed equal to 5.5 x 10-5 meters / second.
• the instantaneous yield R of removing copper from the solution was determined as a function of time, said yield being defined by the expression in which Co and CL respectively denote the concentrations of metal ions in the solution at the inlet and at the outlet of the electrolysis cell.
• the elimination yield is high during the first two hours (of the order of 95%), then it decreases almost linearly to stabilize at the end of the twentieth towards a value of about 50-51%.
• the initial elimination yield had a value equal to 30%, that is to say much lower than the values obtained according to the invention even after a significant duration of the treatment.
• Example 1 was repeated using the percolating porous electrode modified according to the invention, however modifying the flow rate of the peristaltic pump to obtain a circulation speed of the cupric solution in the electrolysis cell equal to 1.98x 10- 4 meter / second.
• the elimination yield is high at the start of the operation, then it decreases more or less linearly to stabilize from the twelfth hour at a value of around 45%.
• the initial elimination yield had a value equal to 33%, c ' that is to say significantly less than the values obtained according to the invention even after a significant duration of the treatment.
• a 0.5 M aqueous potassium sulphate solution containing 1000 p.p.m. of silver ions was treated to recover the silver by electrodeposition.
• the porous fibrous matrix of the percolating porous electrode was constituted by a thick disc 4 millimeters of the felt defined in Example 1 and treated in the same way with the aqueous solution of the surfactant.
• the felt disc impregnated with the surfactant had an apparent density in the wet state relative to water (8M) equal to 1.02.
• the ratio of the apparent density 8M of the felt impregnated in the wet state to the apparent density 80 of the felt not impregnated in the wet state was 2.54.
• An electrolysis potential (electrochemical reduction reaction of silver metal ions) was imposed on the cathode equal to -100 millivolts (relative to the reference electrode).
• the solution to be treated was injected into the electrolysis cell using the peristaltic pump so that said solution percolated through the percolating porous electrode and circulated in said cell with a constant speed equal to 1.98 ⁇ 104 -4 meter / second.
• An electrolysis potential (reduction reaction of lead metal ions) was imposed on the cathode equal to -700 millivolts (relative to the reference electrode), and the flow rate of the peristaltic pump was regulated so that the circulation speed of the solution to be treated in the electrolysis cell was equal to 1.98 ⁇ 10 -4 meters / second.
• This aqueous solution constituted the supernatant of an industrial aqueous effluent subjected to decantation, said effluent having a pH of between 8.5 and 9.
• a potential difference of -2.3 volts was imposed between the anode and the cathode and the flow rate of the peristaltic pump was regulated so that the speed of circulation of the solution to be treated in the electrolysis cell was equal to 1.84 ⁇ 10- 4 meter / second.
• the treated effluent leaving the cell contained 0.05 p.p.m. of cadmium and 0.70 p.p.m. of nickel.
• Discs of a commercial carbon felt having the same characteristics as the felt defined in Example 1 but having a thickness of 10 millimeters, were impregnated by means of the surfactant of Example 1 used in aqueous solution of varying concentration.
• the impregnation was carried out by immersing the felt discs in the appropriate aqueous solution of the surfactant, then quickly rinsing them with distilled water and letting them drain.
• an aqueous solution containing 1000 ppm of cupric ions and 0.5 mole of potassium sulfate was treated to recover the copper by electrodeposition.
• An electrolysis potential (reduction reaction of cupric metal ions) equal to -300 millivolts (relative to the reference electrode) was imposed on the cathode, and the flow rate of the peristaltic pump was regulated so that the circulation speed of the solution to be treated in the electrolysis cell was equal to 1.98 ⁇ 10 -4 meters / second.
• a disc of commercial graphite felt having a thickness of 3.5 millimeters was impregnated with an aqueous solution at 0.1% by weight of the surfactant used in Example 1 by carrying out this impregnation. as shown in said example 1.
• the graphite feture was formed of fibers with a diameter of approximately 9 ⁇ and had the following characteristics:
• the disc impregnated with the surfactant had an apparent density in the wet state relative to water (8M) equal to 1.03.
• the 8M: 80 ratio was 2.50.
• an aqueous solution containing 1000 ppm of cupric ions and 0.5 mole of potassium sulphate was treated to recover the copper by electrodeposition.
• An electrolysis potential equal to -300 millivolts was imposed on the cathode (relative to the reference electrode), and the flow rate of the peristaltic pump was regulated so that the speed of circulation of the solution to be treated in the cell electrolysis was equal to 1,98x 10- 1 meter / second.
• the initial removal yield R m was 99.3%. Furthermore, it was found that in stationary regime, the copper removal efficiency, when the matrix of the percolating porous electrode is an impregnated graphite felt, was higher than that obtained, all the other conditions being equal, using a porous percolating electrode having a matrix constituted by a carbon felt impregnated with the surfactant. However, the clogging of the porous percolating electrode with graphite felt matrix impregnated with surfactant was faster compared to that of the percolating porous electrode with carbon felt matrix impregnated with surfactant.
• An aqueous effluent was treated from the assay of the chemical oxygen demand (COD) of water, said effluent containing by weight 1,700 ppm of Hg ++ ions and 850 ppm of Ag + ions to recover the silver and mercury by electrodeposition.
• COD chemical oxygen demand
• the assay of the chemical oxygen demand of water (assay of the oxidizable materials contained in the water) consists, in principle, of oxidizing by an excess of potassium dichromate, in an acid medium and at boiling, said materials. oxidizable in the presence of silver sulphate (oxidation catalyst) and mercury sulphate (chlorides complexing agent), then to determine the excess of potassium dichromate using a titrated solution of divalent iron sulphate and ammonium.
• an electrolytic cell consisting of a vertical cylindrical enclosure closed at each of its ends, said enclosure having at its lower end an inlet for the effluent to be treated and on its lateral surface two outlets for the treated effluent.
• a cylindrical cathode in the form of a cylindrical porous wall separated the cylindrical enclosure into a central zone, into which the inlet of the enclosure opened and a lateral area communicating with the outlets made in the lateral surface of the enclosure. The separation of the enclosure into two zones by the cathode is such that the liquid arriving in the central zone by the entry of the enclosure percolates through the porous cathode to pass into the lateral zone and from 1 to leave the cell .
• An anode is arranged in the central zone inside the cathode and concentrically with the latter.
• the cathode and the anode are each formed from a modified carbon felt matrix mounted on a support having current leads to the felt.
• the modified matrix consists of a carbon felt, having the characteristics of the carbon felt of example 1, impregnated with the surfactant of example 1, the impregnation technique being analogous to that defined in said example. .
• the matrix of carbon felt impregnated with the surfactant had an apparent density in the wet state relative to water (8M) equal to 1.03 and a ratio of said density to the apparent density in wet state with respect to the water of the non-impregnated felt (80) equal to 2.56.
• a potential difference of -2.4 volts was established between the electrodes and the COD effluent flow rate at the cell inlet was adjusted so that the speed of circulation of said effluent in the cell was equal to 1.31 x 10- 5 meter / second.
• the initial silver removal yield was 99% and that of mercury 98%.
• the synthesis of paraaminophenol was carried out by electroreduction of paranitrophenol, by operating in an electrochemical cell with a percolating porous electrode according to the invention.
• the cell used consisted of a vertical cylindrical enclosure closed at each of its ends and provided with an inlet at its lower end and an outlet at its upper end.
• a percolating porous cathode formed of a modified porous fibrous matrix resting on a platinum ring constituting the current supply, was arranged in the vicinity of the lower part of the enclosure and divided said enclosure into a lower zone communicating with the inlet of the enclosure and an upper zone communicating with the outlet of said enclosure, so that the reaction medium brought into forced flow by the inlet of the enclosure in the lower area of the latter percolated through the cathode to pass in the upper zone and from 1 to the exit of the enclosure.
• the modified porous fibrous matrix of the cathode consisted of a disc of carbon felt impregnated with a surfactant which exhibited the same characteristics as the impregnated disc defined in test IV of Example 6.
• a salt bridge consisting of '' a capillary filled with gelatin saturated with KN0 3 connected the upper zone of the enclosure to an electrode with the saturated calomel serving as reference electrode and an anode consisting of a perforated platinum disc, to allow the passage of the reaction medium and the placement of the salt bridge element present in the enclosure, was arranged above the cathode in a cross section of the enclosure.
• the electrodes were connected to a potentiostat, and a milliammeter was connected in series on the anode circuit between the latter and the potentiostat while a millivolmeter was connected in parallel between the reference electrode and the cathode.
• the reaction medium was brought to the inlet of the cell in forced flow by means of a peristaltic pump.
• the reaction medium used consisted of an aqueous solution at 10% by weight of ethanol containing 5 ⁇ 10 -3 mole of paranitrophenol and 0.3 mole of potassium hydrogen phthalate playing the role of electrolyte, the pH of said solution having been brought to a value of 4.80 by addition of soda.
• a potential of -820 millivolts was imposed on the cathode (relative to the reference electrode), this value having been determined from the intensity / potential curve established for paranitrophenol and corresponding substantially to the average potential of the interval of potential for the diffusion level, and the reaction medium was injected into the enclosure with a constant flow rate equal to 35.4 mi / hour.

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• 1979
  • 1979-12-18 FR FR7930929A patent/FR2472037A1/fr active Granted
• 1980
  • 1980-12-01 EP EP80401715A patent/EP0031267B1/fr not_active Expired
  • 1980-12-01 DE DE8080401715T patent/DE3068623D1/de not_active Expired
  • 1980-12-15 CA CA000366826A patent/CA1156970A/fr not_active Expired
  • 1980-12-16 US US06/216,925 patent/US4330387A/en not_active Expired - Fee Related
  • 1980-12-17 JP JP17964280A patent/JPS5691886A/ja active Pending
  • 1980-12-17 AU AU65481/80A patent/AU536009B2/en not_active Ceased
• 1981
  • 1981-12-03 US US06/326,838 patent/US4396474A/en not_active Expired - Fee Related

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